CN105854330A - Cyclone atomizing vertical sieve plate - Google Patents
Cyclone atomizing vertical sieve plate Download PDFInfo
- Publication number
- CN105854330A CN105854330A CN201610325981.6A CN201610325981A CN105854330A CN 105854330 A CN105854330 A CN 105854330A CN 201610325981 A CN201610325981 A CN 201610325981A CN 105854330 A CN105854330 A CN 105854330A
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- CN
- China
- Prior art keywords
- riser
- gas
- liquid
- under
- cyclone
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/22—Fractionating columns in which vapour bubbles through liquid with horizontal sieve plates or grids; Construction of sieve plates or grids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/30—Fractionating columns with movable parts or in which centrifugal movement is caused
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
- B01J10/02—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor of the thin-film type
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Separating Particles In Gases By Inertia (AREA)
- Cyclones (AREA)
Abstract
The invention discloses a cyclone atomizing vertical sieve plate which is provided with a gas rise pipe arranged on a tray, wherein the lower end of the gas rise pipe extends downwards to a position below the tray; a cyclone is arranged at the lower end of the gas rise pipe; a circle of liquid gap is formed in the pipe wall, in contact with the upper end surface of the tray, of the gas rise pipe. By the use of the cyclone arranged at the lower end of the gas rise pipe, gas entering the gas rise pipe can rise up in a rotatable manner, to drive liquid entering the gas rise pipe from the liquid gap to rise up together, and to form strong tornado type gas-liquid contact; the tensile membrane atomization and mass transfer effect is better than that of the conventional vertical sieve plate. By the arrangement of a collision separator at the upper end of the gas rise pipe, atomized gas flow from the upper end of the gas rise pipe can be better subjected to collision for gas-liquid separation, or a tangent cyclone sheet at the upper part of the gas rise pipe is used for exporting the atomized gas flow in the tangent direction; after the atomized gas flow penetrates through a wire mesh demister at an outlet, gas and liquid are separated, so that the atomization mass transfer process is extended, and an extremely good gas-liquid separation effect is further achieved.
Description
Technical field
The present invention relates to the vertical sieve tray on a kind of chemical industry tower tray, specifically, it is a kind of eddy flow mist
Change vertical tower tray.
Background technology
As it is shown in figure 9, existing vertical sieve tray is to be provided with several riseies (20) on tower tray (6),
Leaving liquid seam (21) between its lower end and tower tray, its top is provided with sieve aperture (22), and top is shut.Work
When making, the liquid on tower tray flows into riser by its liquid seam (21), by from the gas below tower tray
Body membrane, atomization, complete mass transport process in riser, and the gas-liquid mixed phase after mass transfer is from riser
The sieve aperture ejection in portion, wherein gas continues to rise, and drop falls in the liquid on tower tray.Vertical sieve tray
Utilize membrane atomization to define preferable gas-liquid contact in riser, thus achieve good mass transfer
Effect.But expect that more preferable mass transfer effect is the target that this area is constantly pursued, although vertical sieve tray takes
Obtaining good mass transfer effect, but it is without eddy flow, in sieve plate, gas rises naturally, compares eddy flow
From the point of view of, they on the severity of gas-liquid contact time and gas-liquid contact all relative mistake some；Furthermore,
After existing vertical sieve tray atomization air flow is formed in riser, directly from sieve aperture out, do not separated
Journey, therefore, existing vertical sieve tray is not reaching to even more ideal mass transfer and separating effect.
Summary of the invention
It is an object of the invention to the present situation for prior art, it is provided that a kind of swirling flow atomizing vertical sieve tray,
First it is in vertical sieve tray, to realize gas rotation eddy flow rise, strengthens atomization mass transfer effect, then in rotation
On the basis of stream atomization, strengthen gas-liquid separation process.
For achieving the above object, first technical scheme of the present invention is as follows:
It has a riser being located on column plate, and the upper surface of this riser is closed, and at a liter gas
Having sieve aperture on the tube wall of pipe top, it is characterized in that: extend under column plate under described riser lower end
Side, and under riser, in end tube section, it is provided with a cyclone, in described riser and tower tray upper surface
The tube wall of contact has liquid seam for one week.
The technical scheme that the present invention the first technical scheme is improved is:
Described cyclone is a fan blade, a spiral board or is located at end tube section pipe under riser
The wall inscribe spinning disk of a week.
Second technical scheme of the present invention is as follows:
It has a riser being located on column plate, extends below column plate under this riser lower end, and
Under this riser, in end tube section, it is provided with a cyclone, contacts with tower tray upper surface at described riser
Tube wall within one week, have liquid seam, described riser upper surface is open shape, and in this riser upper end
Being provided with an impaction separator, described impaction separator is fixed on riser by gusset.
The technical scheme that the present invention the second technical scheme is improved is as follows:
Described cyclone is a fan blade, a spiral board or is located at end tube section pipe under riser
The wall inscribe spinning disk of a week.
Under described riser, end tube section is undergauge pipeline section, and on this undergauge pipeline section and riser column plate
The diameter ratio of square tube section is 0.15～0.95.
3rd technical scheme of the present invention is as follows:
It has a riser being located on column plate, extends below column plate under this riser lower end, and
Under this riser, in end tube section, it is provided with a cyclone, contacts with tower tray upper surface at described riser
Tube wall within one week, have liquid seam, the upper end actinal surface at described riser be provided with one capping plate, described
Riser upper end tube wall within one week, be provided with circumscribed spinning disk, and set on the circumference of this circumscribed spinning disk
There is wire mesh demister.
The technical scheme that the present invention the 3rd technical scheme is improved is as follows:
Described cyclone is a fan blade, a spiral board or is located at end tube section pipe under riser
The wall inscribe spinning disk of a week.
Under described riser, end tube section is undergauge pipeline section, and on this undergauge pipeline section and riser column plate
The diameter ratio of square tube section is 0.15～0.95.
Above described riser column plate, the lower end of pipeline section is provided with the changeover portion of described undergauge pipeline section.
Being found out by technique scheme, the present invention is provided with one in the riser lower end of vertical sieve tray
Cyclone, makes the gas rotating of entrance riser rise, and the gas that this rotation rises carries from liquid meets
Enter the liquid in riser and rotate rising together, form the gas-liquid fierceness contact of tornado, and
There is vertical sieve tray to compare, enhance the mass transfer effect of membrane atomization.On this basis, in order to strengthen gas
Liquid separates, and second technical scheme of the present invention utilizes the impaction separator arranged in riser upper end, makes
From riser upper end, atomization air flow out has obtained good gas-liquid separation by collision；Furthermore, also
Being to strengthen gas-liquid separation process, the 3rd technical scheme of the present invention is to utilize on riser top
Atomization air flow is tangentially derived by circumscribed spinning disk, maintains it to rotate situation and does not subtracts, makes atomization air flow rotate
Collision type carries out gas-liquid separation through wire mesh demister, and this not only has good gas-liquid separation effect,
The most also continue mass transport process.
Accompanying drawing explanation
Fig. 1, the structure of the embodiment of the present invention 1 and operating diagram.
Fig. 2, one of structure (the A-A section of Fig. 1) schematic diagram of cyclone.
Fig. 3, cyclone structure (the A-A section of Fig. 1) schematic diagram two.
Fig. 4, cyclone structure (main regard) schematic diagram three.
The B-B cross-sectional schematic of Fig. 5, Fig. 4.
Fig. 6, the structure of the embodiment of the present invention 2 and operating diagram.
Fig. 7, the structure of the embodiment of the present invention 3 and operating diagram.
The plan structure schematic diagram of Fig. 8, Fig. 7.
Fig. 9, existing vertical sieve tray structure and operating diagram.
Detailed description of the invention
Embodiment 1
Seeing Fig. 1, it has a riser (1) being located on column plate (6), this riser upper
End face is closed, and has sieve aperture (1-1) on the tube wall of riser top, under described riser lower end
Extend below column plate, and under riser, in end tube section, be provided with a cyclone (2), at described liter of gas
The tube wall that pipe contacts with tower tray upper surface has liquid seam (3) for one week.
Seeing Fig. 2, the cyclone described in Fig. 1 can use an existing fan blade (7), this fan blade
Wheel can be fixing, it is also possible to is to rotate.If fan blade is to rotate, when gas is from a liter gas
When infratubal port pours riser, this fan blade is blown rotation by gas, and the fan blade of rotation drives again
Gas rotating, makes the gas rotating of entrance riser rise.If fan blade is fixing, work as gas
From riser lower port through fan blade, whirlwind can be formed along with the guiding of fan blade and rise.
Seeing Fig. 3, the cyclone described in Fig. 1 can also use an existing spiral board (8), its
Act on identical with fixing fan blade.
See Fig. 4,5, the cyclone described in Fig. 1 can also be to be located at end tube section tube wall under riser
The inscribe spinning disk (1-2) of one week.The gas of upper punch leading along inscribe spinning disk below riser
To and form rising swirling eddy.
The course of work of this example is: seeing Fig. 1, the gas that tower tray (6) lower section rises is through cyclone
(2), making gas rotating increase, liquid seam (3) from riser of the liquid on tower tray (6) enters
Riser, thus the gas cyclone atomization mass transfer risen by rotation, gas-liquid two-phase has carried out tornado
Fierce contact, the dynamics of gas-liquid contact time and gas-liquid collision is all long than vertical sieve tray, fierce,
Therefore, the effect of gas-liquid mass transfer is better than vertical sieve tray.
Embodiment 2
Seeing Fig. 6, it has a riser (1) being located on column plate (6), this riser lower end
Under extend below column plate, and under this riser, in end tube section, be provided with a cyclone (2), described
The tube wall that riser contacts with tower tray upper surface has liquid seam (3), described riser upper surface for one week
For opening shape, and being provided with an impaction separator (4) in this riser upper end, described collision separates
Device (4) is fixed on riser (1) by gusset (5).In order to extend the gas-liquid of impaction separator
Defiber, strengthens mass transport process, and the spherical crown lower edge of described impaction separator is zigzag.This example
The structure of cyclone (2) is same as in Example 1.
During work, anterior mass transport process is same as in Example 1, the gas that i.e. tower tray (6) lower section rises
Through cyclone (2), making gas rotating increase, the liquid on tower tray (6) is from riser tube wall
Liquid seam (3) enters riser, thus the gas rotating risen by rotation is atomized mass transfer；Then atomization gas
Stream is gone out from the top of riser (1), collides on described impaction separator (4), carries out gas
Liquid separates, and the gas phase of collision rift is gone out from the zigzag lower edge of impaction separator and continuously risen to
Layer tower tray, its liquid phase sawtooth point in impaction separator lower edge drips, and returns on this layer of tower tray
In liquid.The collision through impaction separator (4) of the above-mentioned atomization air flow gone out from riser top,
Strengthen gas-liquid separation process, and not this collision separation process of existing vertical sieve tray, therefore, its
The gas-liquid separation degree of atomization air flow is less than this example.
Embodiment 3
See Fig. 7,8, it has a riser (1) being located on column plate (6), under this riser
Extend below column plate under end, and under this riser, in end tube section, be provided with a cyclone (2), in institute
State the tube wall that riser contacts with tower tray upper surface and within one week, have liquid seam (3), upper at described riser
Port surface be provided with one capping plate (9), make this upper end actinal surface for being sealed shape, on described riser
Within one week, it is provided with circumscribed spinning disk (1-3) on end tube wall, and is provided with on the circumference of this circumscribed spinning disk
Wire mesh demister (10).The structure of the cyclone (2) of this example is same as in Example 1.
During work, anterior mass transport process is same as in Example 1, the gas that i.e. tower tray (6) lower section rises
Through cyclone (2), making gas rotating increase, the liquid on tower tray (6) is from riser tube wall
Liquid seam (3) enters riser, thus the gas rotating risen by rotation is atomized mass transfer, then goes up
The atomization air flow on riser top, through the guiding of circumscribed spinning disk (1-3), rotary removes through silk screen
Foam device (10) gas-liquid separation afterwards, gas rises to upper strata tower tray, liquid phase at wire mesh demister lower,
Return in the liquid on this layer of tower tray.This example continue for the rotation of riser top atomization air flow, makes
Atomization air flow rotary collision formula carries out gas-liquid separation through wire mesh demister, and this not only has good gas
Liquid separating effect, has the most also continued mass transport process.Referring back to Fig. 6,7, in order to further enhance rotation
Stream, under described riser, end tube section can be undergauge pipeline section, pipeline section above this undergauge pipeline section and column plate
Diameter ratio be 0.15～0.95.
Referring back to Fig. 7, above described riser column plate, the lower end of pipeline section can be provided with described undergauge pipeline section
(1-4) changeover portion (1-5), so, can improve the liquid measure that liquid seam (3) sucks, be conducive to
Gas-liquid mass transfer.It addition, be riser easy to process, described can be upper and lower with column plate as boundary
Two-stage structure, this two-stage structure all can use gusset (11) to be fixed on tower tray.
Claims (9)
1. a swirling flow atomizing vertical sieve tray, it has a riser (1) being located on column plate (6),
The upper surface of this riser is closed, and has sieve aperture (1-1), its feature on the tube wall of riser top
It is: extend below column plate under described riser lower end, and is provided with one in end tube section under riser
Cyclone (2), the tube wall contacted with tower tray upper surface at described riser has liquid seam (3) for one week.
Swirling flow atomizing vertical sieve tray the most according to claim 1, is characterized in that: described eddy flow
Device is a fan blade (7), a spiral board (8) or is located at end tube section tube wall one week under riser
Inscribe spinning disk (1-2).
3. a swirling flow atomizing vertical sieve tray, is characterized in that: it has one and is located on column plate (6)
Riser (1), extend below column plate under this riser lower end, and under this riser in end tube section
Being provided with a cyclone (2), the tube wall contacted with tower tray upper surface at described riser has liquid in one week
Seam (3), described riser upper surface is open shape, and is provided with a collision in this riser upper end
Separator (4), described impaction separator (4) is fixed on riser (1) by gusset (5).
Swirling flow atomizing vertical sieve tray the most according to claim 3, is characterized in that: described eddy flow
Device is a fan blade (7), a spiral board (8) or is located at end tube section tube wall one week under riser
Inscribe spinning disk (1-2).
5., according to the swirling flow atomizing vertical sieve tray described in claim 3 or 4, it is characterized in that: described
Under riser, end tube section is undergauge pipeline section, and pipeline section straight above this undergauge pipeline section and riser column plate
The ratio in footpath is 0.15～0.95.
6. a swirling flow atomizing vertical sieve tray, is characterized in that: it has one and is located on column plate (6)
Riser (1), extend below column plate under this riser lower end, and under this riser in end tube section
Being provided with a cyclone (2), the tube wall contacted with tower tray upper surface at described riser has liquid in one week
Seam (3), the upper end actinal surface at described riser is provided with capping plate (9), at described riser
One week of upper end tube wall is provided with circumscribed spinning disk (1-3), and is provided with on the circumference of this circumscribed spinning disk
Wire mesh demister (10).
Swirling flow atomizing vertical sieve tray the most according to claim 6, is characterized in that: described eddy flow
Device is a fan blade (7), spiral board (8) or is located at the interior of end tube section tube wall under riser one week
Cut spinning disk (1-2).
8., according to the swirling flow atomizing vertical sieve tray described in claim 6 or 7, it is characterized in that: described
Under riser, end tube section is undergauge pipeline section (1-4), and square tube on this undergauge pipeline section and riser column plate
The diameter ratio of section is 0.15～0.95.
Swirling flow atomizing vertical sieve tray the most according to claim 8, is characterized in that: at described liter of gas
Above pipe column plate, the lower end of pipeline section is provided with the changeover portion (1-5) of described undergauge pipeline section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610325981.6A CN105854330A (en) | 2016-05-17 | 2016-05-17 | Cyclone atomizing vertical sieve plate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610325981.6A CN105854330A (en) | 2016-05-17 | 2016-05-17 | Cyclone atomizing vertical sieve plate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105854330A true CN105854330A (en) | 2016-08-17 |
Family
ID=56634147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610325981.6A Pending CN105854330A (en) | 2016-05-17 | 2016-05-17 | Cyclone atomizing vertical sieve plate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105854330A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112221285A (en) * | 2020-08-20 | 2021-01-15 | 苏州乔发环保科技股份有限公司 | Foam catching device for gas-liquid separator |
| CN112439309A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Acrylonitrile device rapid cooling system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5635145A (en) * | 1994-08-23 | 1997-06-03 | Shell Oil Company | Multi-bed downflow reactor |
| JP2007029936A (en) * | 2005-07-22 | 2007-02-08 | Anemosu:Kk | Mixing element and static fluid mixer using the same |
| CN102397709A (en) * | 2010-09-15 | 2012-04-04 | 中国石油天然气股份有限公司 | Modular catalyst filling structure of vertical sieve plate |
| CN203610019U (en) * | 2013-10-14 | 2014-05-28 | 航天环境工程有限公司 | Cyclone distillation desorption column |
| CN104606962A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Straight cylinder-shaped flow baffling demister |
-
2016
- 2016-05-17 CN CN201610325981.6A patent/CN105854330A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5635145A (en) * | 1994-08-23 | 1997-06-03 | Shell Oil Company | Multi-bed downflow reactor |
| JP2007029936A (en) * | 2005-07-22 | 2007-02-08 | Anemosu:Kk | Mixing element and static fluid mixer using the same |
| CN102397709A (en) * | 2010-09-15 | 2012-04-04 | 中国石油天然气股份有限公司 | Modular catalyst filling structure of vertical sieve plate |
| CN203610019U (en) * | 2013-10-14 | 2014-05-28 | 航天环境工程有限公司 | Cyclone distillation desorption column |
| CN104606962A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Straight cylinder-shaped flow baffling demister |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112439309A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Acrylonitrile device rapid cooling system |
| CN112221285A (en) * | 2020-08-20 | 2021-01-15 | 苏州乔发环保科技股份有限公司 | Foam catching device for gas-liquid separator |
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Application publication date: 20160817 |